WO2021047146A1 - 一种含乙二醇的工业尾气的处理系统及其使用方法 - Google Patents

一种含乙二醇的工业尾气的处理系统及其使用方法 Download PDF

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WO2021047146A1
WO2021047146A1 PCT/CN2020/076453 CN2020076453W WO2021047146A1 WO 2021047146 A1 WO2021047146 A1 WO 2021047146A1 CN 2020076453 W CN2020076453 W CN 2020076453W WO 2021047146 A1 WO2021047146 A1 WO 2021047146A1
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condenser
ethylene glycol
tail gas
gas containing
industrial tail
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PCT/CN2020/076453
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English (en)
French (fr)
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方华玉
陈锦程
朱恩斌
王读彬
余国清
李天源
吴建通
陈建华
林胜尧
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艾凡佳德(上海)环保科技有限公司
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Publication of WO2021047146A1 publication Critical patent/WO2021047146A1/zh

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0033—Other features
    • B01D5/0036—Multiple-effect condensation; Fractional condensation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1406—Multiple stage absorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1487—Removing organic compounds
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
    • C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
    • C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
    • C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
    • C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
    • C07C29/86—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by liquid-liquid treatment

Definitions

  • the present invention belongs to the processing field of industrial tail gas, and more specifically relates to a processing system of industrial tail gas containing ethylene glycol and a method of use thereof.
  • Polyester is a polymer compound prepared by esterification and polycondensation of purified terephthalic acid (PTA) and ethylene glycol (EG). It is widely used in textiles, packaging, electronics, electrical appliances, Medical equipment, construction, automobiles and other fields. However, a large amount of tail gas is produced during the production process, which has a great impact on the environment, especially the tail gas containing ethylene glycol.
  • the ethylene glycol causes high COD in wastewater.
  • the non-condensable gas aldehydes in the tail gas pollute the atmosphere seriously.
  • the tiny particles in the tail gas are An important factor affecting PM2.5.
  • most polyester plants have adopted spraying, burning and other treatment measures for exhaust gas treatment.
  • the COD of wastewater is as high as 20000 ⁇ 30000mg/L after direct spraying.
  • the cost of wastewater treatment is high, but it is also important for the important chemical industry that can be recycled and reused.
  • the raw material ethylene glycol is also a great loss.
  • most factories use the hot coal furnace combustion method. Due to the low combustion temperature, it cannot achieve complete harmless treatment, and the ethylene glycol contained in the exhaust gas cannot be treated. Reuse in polyester production is also a huge waste for enterprises.
  • the present invention provides a treatment system for industrial tail gas containing ethylene glycol, including a ethylene glycol injection collector, a ethylene glycol storage tank, a first circulating pump, a first condenser, and a second condenser ,
  • the third condenser, the leaching tower and the adsorption device, the glycol spray collector is set on the top of the glycol storage tank, and is connected to the first condenser, the first circulating pump and the glycol storage tank ,
  • the top of the ethylene glycol storage tank is provided with a gas outlet, a second condenser liquid phase reflux port, and a third condenser liquid phase reflux port.
  • the gas outlet, the second condenser and the second condenser liquid phase reflux port are phased And the second condenser gas phase outlet, the third condenser, and the third condenser liquid phase reflux port are connected, the third condenser is connected to the rinsing tower and the adsorption device in sequence, the The leaching tower is connected with the first circulating pump.
  • the present invention provides a method for processing industrial exhaust gas containing ethylene glycol by the processing system, which includes the following steps:
  • Cooling the pre-cooled industrial tail gas containing condensed ethylene glycol, and the cooling is carried out by sequentially sending to the second condenser and the third condenser to obtain the low-temperature industrial tail gas containing ethylene glycol;
  • the tail gas of the spray tower is sent to an adsorption device for further adsorption and removal of impurities, and then burned and discharged through a heat-conducting oil furnace.
  • the cooled low-temperature industrial tail gas is sprayed with water in the leaching tower, which can remove various water-soluble organic matter including ethylene glycol, and reduce the content of organic matter in the tail gas at the outlet of the leaching tower. COD content in wastewater;
  • the tail gas is adsorbed by the activated carbon adsorption device, which further captures the organic matter and tiny particles in the tail gas, so that the impurities in the tail gas are lower.
  • Fig. 1 is a schematic diagram of a processing system for industrial exhaust gas containing ethylene glycol according to a specific embodiment of the present invention.
  • a treatment system for industrial exhaust gas containing ethylene glycol including a ethylene glycol injection collector, a ethylene glycol storage tank, a first circulating pump, a first condenser, and a second condenser ,
  • the third condenser, the leaching tower and the adsorption device, the glycol spray collector is set on the top of the glycol storage tank, and is connected to the first condenser, the first circulating pump and the glycol storage tank ,
  • the top of the ethylene glycol storage tank is provided with a gas outlet, a second condenser liquid phase reflux port, and a third condenser liquid phase reflux port.
  • the gas outlet, the second condenser and the second condenser liquid phase reflux port are phased And the second condenser gas phase outlet, the third condenser, and the third condenser liquid phase reflux port are connected, the third condenser is connected to the rinsing tower and the adsorption device in sequence, the The leaching tower is connected with the first circulating pump.
  • the industrial tail gas containing ethylene glycol is directly sent to the glycol spray collector at the top of the glycol storage tank, contacts with the ethylene glycol circulating in the glycol spray collector, and enters together with the sprayed ethylene glycol
  • the ethylene glycol storage tank, the ethylene glycol storage tank, the first circulating pump, and the first condenser are connected and conducted by a pipeline, and the ethylene glycol in the tail gas is recovered by the sprayed ethylene glycol cooling and condensation
  • the uncondensed tail gas enters the second condenser from the outlet, and the ethylene glycol in the tail gas is further condensed and recovered in the second condenser, and flows into the ethylene glycol through the liquid phase reflux port of the second condenser.
  • the tail gas that does not condense in the second condenser continues to enter the third condenser to be further cooled and condensed and recovered.
  • the tail gas from the third condenser enters the leaching tower, and water spraying is carried out in the leaching tower.
  • the tail gas from the outlet of the leaching tower enters the adsorption device for further adsorption and removal of impurities.
  • the second condenser is cooled by circulating cooling water, and the temperature of the circulating cooling water is ⁇ 35°C.
  • the third condenser adopts chilled water for cooling, and the chilled water temperature is 7-12°C.
  • the eluate discharged from the bottom of the leaching tower can be returned to the leaching tower to participate in the leaching process, so as to save the use of spray water.
  • the sewage is regularly discharged into the sewage treatment system for treatment. After the sprinkling water drains the sewage, it is supplemented with fresh industrial water, thereby improving the treatment effect and reducing the operating cost.
  • the outlet of the leaching tower is also connected to the spray inlet of the leaching tower through a second circulating pump.
  • an adsorption device with better organic matter adsorption effect is selected.
  • the adsorption device is an activated carbon adsorber.
  • Cooling the pre-cooled industrial tail gas containing condensed ethylene glycol, and the cooling is carried out by sequentially sending to the second condenser and the third condenser to obtain the low-temperature industrial tail gas containing ethylene glycol;
  • the tail gas of the spray tower is sent to an adsorption device for further adsorption and removal of impurities, and then burned and discharged through a heat-conducting oil furnace.
  • the ethylene glycol circulating in the ethylene glycol jet collector can be condensed to recover part of the ethylene glycol in the industrial tail gas.
  • the second condenser and the third condenser are condensation treatments with different temperature gradient ranges, and water is used in the leaching tower for leaching.
  • the ethylene glycol in the ethylene glycol-containing industrial tail gas has been fully condensed and recovered, and the soluble organic matter has been basically removed.
  • the method of burning and discharging heat conduction oil furnace is the common industrial tail gas in the chemical industry.
  • One of the treatment methods, in this treatment process is a harmless treatment method.
  • the second condenser is cooled by circulating cooling water, and the cooling water temperature is ⁇ 32°C.
  • the third condenser uses chilled water for cooling, and the chilled water has a water temperature of 7-12°C.
  • the leaching tower is rinsed with more than 3 layers of water, preferably 3-9 layers.
  • the adsorption device is an activated carbon adsorber.
  • this embodiment provides a rectification system for industrial tail gas containing ethylene glycol, which includes an ethylene glycol storage tank 10, an ethylene glycol injection collector 101, a first circulating pump 11, and a first condenser 12 , The second condenser 21, the third condenser 22, the rinse tower 30, the second circulating pump 31 and the activated carbon adsorber 40.
  • the glycol injection collector 101 is arranged on the top of the glycol storage tank 10, and the first condenser 12, the first circulating pump 11, the glycol storage tank 10, and the glycol injection collector 101 are connected. .
  • the top of the ethylene glycol storage tank 10 is provided with a second condenser liquid phase reflux port 102, a third condenser liquid phase reflux port 103, and an air outlet 104.
  • the air outlet 104, the second condenser 21, and the second condenser liquid phase reflux port 102 are connected, and the second condenser gas phase outlet (not marked in the figure), the third condenser 22, and the third condenser
  • the liquid phase reflux port 103 of the reactor is connected, the third condenser 22 is connected to the leaching tower 30 and the activated carbon adsorber 40 in sequence, and the leaching tower 30 is connected to the first circulating pump 11.
  • the industrial exhaust gas containing ethylene glycol is directly sent to the glycol spray collector 101 at the top of the glycol storage tank 10, and contacts with the ethylene glycol circulating in the glycol spray collector 10, and with the sprayed ethylene glycol.
  • Alcohol enters the ethylene glycol storage tank 10 together.
  • the ethylene glycol storage tank 10, the first circulating pump 11 and the first condenser 12 are connected and conducted by a pipeline, and the ethylene glycol in the tail gas is passed by the first condenser
  • the ethylene glycol sprayed in the internal circulation is cooled and condensed and recovered into the ethylene glycol storage tank 10.
  • the uncondensed tail gas enters the second condenser 21 from the outlet 104 at the top of the ethylene glycol storage tank 10, and the ethylene glycol in the tail gas is in the second condenser 21.
  • the second condenser 21 is further condensed and recovered, and flows into the ethylene glycol storage tank 10 through the liquid phase reflux port 102 of the second condenser.
  • the uncondensed tail gas in the second condenser 21 continues to enter the third condenser 22 for further cooling and condensation
  • the tail gas from the third condenser 22 enters the leaching tower 30, and water spraying is performed in the leaching tower 30 to capture organic matter and fine particles.
  • the tail gas from the outlet of the leaching tower 30 enters the activated carbon adsorber 40 for processing. Further adsorption and impurity removal.
  • the outlet of the leaching tower 30 is also connected to the spray inlet of the leaching tower 30 through the second circulating pump 31.
  • the method for purifying industrial tail gas containing ethylene glycol using the treatment system for industrial tail gas containing ethylene glycol provided by the above technical scheme is as follows:
  • the industrial exhaust gas containing ethylene glycol is directly sent to the ethylene glycol jet collector at the top of the ethylene glycol storage tank, contacts with the ethylene glycol circulating in the ethylene glycol jet collector, and interacts with the injected ethylene glycol.
  • the alcohol enters the glycol storage tank together.
  • the temperature of industrial tail gas containing ethylene glycol can drop from 150°C above the exit of the previous process to 40-70°C, and 90% of the ethylene glycol in the tail gas will be sprayed and captured into the ethylene glycol storage tank.
  • the 40-70°C ethylene glycol is pumped into the first condenser 12 through the first circulating pump 11 to be cooled to 20-35°C (to obtain the pre-cooled industrial tail gas containing ethylene glycol) and enter the next "spray-spray capture" recycle.
  • Pre-cooling industrial tail gas containing ethylene glycol enters the second condenser, and then enters the third condenser, where the ethylene glycol in the industrial tail gas is condensed and recovered.
  • the second condenser is cooled with 32°C circulating cooling water
  • the third condenser is cooled with 7°C chilled water. So far, the pre-cooling industrial tail gas containing ethylene glycol is sequentially cooled to 30-45°C and 10-30°C after the heat exchange of cooling water and chilled water. After this process, the industrial tail gas containing ethylene glycol is pre-cooled again. Part of the ethylene glycol is condensed and recycled to the ethylene glycol storage tank.
  • the tail gas from the third condenser enters the leaching tower for water spray capture.
  • the upper part of the leaching tower is equipped with 3-9 layers of water spray heads, and the water is sprayed through the second circulating pump to realize the circulation of water.
  • Organic matter in the exhaust gas is captured by water. When the organic matter concentration of the sewage at the outlet of the leaching tower is high, it will be discharged regularly.
  • the tail gas from the leaching tower enters the activated carbon adsorption device for adsorption and impurity removal.
  • the concentration of organic matter in the tail gas can be reduced to below 5%, and the recycling rate of ethylene glycol is above 98%.

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  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
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Abstract

一种含乙二醇的工业尾气的处理系统和方法，该系统包括乙二醇喷射收集器（101）、乙二醇储罐（10）、第一循环泵（11）、第一冷凝器（12）、第二冷凝器（21）、第三冷凝器（22）、淋洗塔（30）和吸附装置，乙二醇喷射收集器（101）设置在乙二醇储罐（10）顶部，并与第一冷凝器（12）、第一循环泵（11）和乙二醇储罐（10）相导通，乙二醇储罐（10）顶端开设出气口（104）、第二冷凝器液相回流口（102）、第三冷凝器液相回流口（103），出气口（104）、第二冷凝器（21）和第二冷凝器液相回流口（102）相导通，且第二冷凝器气相出口、第三冷凝器（22）和第三冷凝器液相回流口（103）相导通，第三冷凝器（22）与淋洗塔（30）和吸附装置依序接通，淋洗塔（30）与第一循环泵（11）相接通。

Description

一种含乙二醇的工业尾气的处理系统及其使用方法 技术领域
本发明属于工业尾气的处理领域，更具体地涉及一种含乙二醇的工业尾气的处理系统及其使用方法。
背景技术
聚酯(PET)是由精对苯二甲酸(PTA)和乙二醇(EG)经过酯化、缩聚反应制备而成的一种高分子化合物，其广泛应用于纺织、包装、电子、电器、医疗器械、建筑、汽车等领域。然而其生产过程中产生大量尾气，对环境影响很大，特别是含乙二醇的尾气，乙二醇导致废水COD很高，尾气中不凝气体醛类对大气污染严重，尾气中微小粒子是影响PM2.5的重要因子。目前大多聚酯工厂对尾气处理都采用了喷淋、燃烧等处理措施，但因直接喷淋后造成废水COD高达20000～30000mg/L，后期不仅废水处理成本高，对于可以回收再利用的重要化工原料乙二醇也是一种极大的损耗，目前大部分工厂都采用的进热煤炉燃烧法，由于燃烧温度低，不能达到彻底无害化处理，且尾气中的所含乙二醇成分不能再利用于聚酯生产，对企业来说也是一种巨大浪费。
发明内容
鉴于背景技术中存在的技术问题，需要提供一种含乙二醇的工业尾气的处理系统及其使用方法，该系统需要兼具净化处理含乙二醇的工业尾气和有效回收利用乙二醇(EG)的功能。
为实现上述目的，本发明提供了一种含乙二醇的工业尾气的处理系统，包括乙二醇喷射收集器、乙二醇储罐、第一循环泵、第一冷凝器、第二冷凝 器、第三冷凝器、淋洗塔和吸附装置，所述乙二醇喷射收集器设置在乙二醇储罐顶部，并与第一冷凝器、第一循环泵和乙二醇储罐相导通，所述乙二醇储罐顶端开设出气口、第二冷凝器液相回流口、第三冷凝器液相回流口，所述出气口、第二冷凝器和第二冷凝器液相回流口相导通，且所述第二冷凝器气相出口、第三冷凝器和第三冷凝器液相回流口相导通，所述第三冷凝器与淋洗塔和吸附装置依序接通，所述淋洗塔与第一循环泵相接通。
在本发明的第二方面，本发明提供所述的处理系统处理含乙二醇的工业尾气的方法，包括以下步骤：
将含乙二醇的工业尾气送入乙二醇喷射收集器，同乙二醇喷射收集器循环的乙二醇进行接触，得到预降温的、且含凝结乙二醇的工业尾气；
将所述预降温的、且含凝结乙二醇的工业尾气进行冷却，所述冷却为依次送入第二冷凝器、第三冷凝器，得到低温含乙二醇的工业尾气；
将所述低温含乙二醇的工业尾气送入淋洗塔淋洗，得到喷淋塔尾气；
将所述喷淋塔尾气送入吸附装置进一步吸附除杂后通过导热油炉燃烧排放。
区别于现有技术，上述技术方案至少存在以下有益效果：
1、通过第一冷凝器、第二冷凝器以及第三冷凝器的降温，尾气中98％以上的乙二醇被捕捉、回收进入乙二醇储罐再利用，大大减少了原料的浪费、降低了成本；
2、经过降温的低温工业尾气通过淋洗塔的水喷淋，能够去除含乙二醇在内的可溶于水的各类有机物，降低了淋洗塔出口处尾气中的有机物含量，降低了废水中COD含量；
3、尾气通过活性炭吸附装置吸附，进一步捕捉了尾气中的有机物和微小颗粒，使得尾气中杂质成分更低。
附图说明
图1为本发明具体实施方式所述一种含乙二醇的工业尾气的处理系统示意图。
附图标记说明：
10、乙二醇储罐；
11、第一循环泵；
12、第一冷凝器；
101、乙二醇喷射收集器；
102、第二冷凝器液相回流口；
103、第三冷凝器液相回流口；
104、出气口；
21、第二冷凝器；
22、第三冷凝器；
30、淋洗塔；
31、第二循环泵；
40、活性炭吸附器。
具体实施方式
下面详细说明本发明的一种含乙二醇的工业尾气的处理系统及其使用方法。
首先说明本发明第一方面，即一种含乙二醇的工业尾气的处理系统，包括乙二醇喷射收集器、乙二醇储罐、第一循环泵、第一冷凝器、第二冷凝器、第三冷凝器、淋洗塔和吸附装置，所述乙二醇喷射收集器设置在乙二醇储罐顶部，并与第一冷凝器、第一循环泵和乙二醇储罐相导通，所述乙二醇储罐顶端开设出气口、第二冷凝器液相回流口、第三冷凝器液相回流口，所述出气口、第二冷凝器和第二冷凝器液相回流口相导通，且所述第二冷凝器气相 出口、第三冷凝器和第三冷凝器液相回流口相导通，所述第三冷凝器与淋洗塔和吸附装置依序接通，所述淋洗塔与第一循环泵相接通。
所述含有乙二醇的工业尾气直接送到乙二醇储罐顶端的乙二醇喷射收集器，同乙二醇喷射收集器循环的乙二醇进行接触，并与喷射的乙二醇一同进入所述乙二醇储罐，所述乙二醇储罐、第一循环泵及第一冷凝器之间由管道相连接导通，尾气中的乙二醇被喷射的乙二醇降温冷凝回收到乙二醇储罐中，未凝结的尾气从出气口进入第二冷凝器，尾气中的乙二醇在第二冷凝器又得到进一步冷凝回收，经第二冷凝器液相回流口流入乙二醇储罐，在第二冷凝器中不凝结的尾气继续进入第三冷凝器，得到进一步降温冷凝回收，从第三冷凝器出来的尾气进入淋洗塔，在淋洗塔内进行水喷淋，以捕捉有机物和微小颗粒，从淋洗塔出口出来的尾气进入吸附装置进行进一步吸附除杂。
优选地，所述第二冷凝器采用循环冷却水降温，所述循环冷却水的水温≤35℃。
优选地，所述第三冷凝器采用冷冻水降温，所述冷冻水水温为7-12℃。
进一步地，淋洗塔底部排出的淋洗液可以重新回到淋洗塔参与淋洗过程，达到节约使用喷淋水的目的，同时根据废水中有机物含量定期排除污水进入污水处理系统进行处理，喷淋水排除污水后用新鲜工业水进行补充，从而提高处理效果和降低运行成本。
优选地，所述淋洗塔的出口还通过第二循环泵接通至淋洗塔喷淋入口。
进一步地，为使排入油炉焚烧的含乙二醇的工业尾气的有机物浓度和成分降到最低，选择对有机物吸附效果较好的吸附装置。
优选地，所述吸附装置为活性炭吸附器。
其次说明本发明第二方面，即采用本发明第一方面所述的处理系统处理含乙二醇的工业尾气的方法，其中，包括以下步骤：
将含乙二醇的工业尾气送入乙二醇喷射收集器，同乙二醇喷射收集器循环的乙二醇进行接触，得到预降温的、且含凝结乙二醇的工业尾气；
将所述预降温的、且含凝结乙二醇的工业尾气进行冷却，所述冷却为依次送入第二冷凝器、第三冷凝器，得到低温含乙二醇的工业尾气；
将所述低温含乙二醇的工业尾气送入淋洗塔淋洗，得到喷淋塔尾气；
将所述喷淋塔尾气送入吸附装置进一步吸附除杂后通过导热油炉燃烧排放。
乙二醇喷射收集器循环的乙二醇可冷凝回收部分工业尾气中的乙二醇，第二冷凝器和第三冷凝器为不同温度梯度范围的冷凝处理，淋洗塔内采用水进行淋洗，吸附装置内吸附之后所述含乙二醇的工业尾气中的乙二醇已得到充分的冷凝回收，并且可溶有机物也已基本去除，导热油炉燃烧排放的方法是化工领域常见的工业尾气处理处置方法之一，在此处理工艺中为无害化处理方式。
优选地，所述第二冷凝器采用循环冷却水降温，所述冷却水水温≤32℃。
更加优选地，所述第三冷凝器采用冷冻水降温，所述冷冻水的水温为7-12℃。
优选地，所述淋洗塔采用3层以上的水淋洗，优选为3-9层。
优选地，所述吸附装置为活性炭吸附器。
为详细说明技术方案的技术内容、构造特征、所实现目的及效果，以下结合具体实施例详予说明。应理解，这些实施例仅用于说明本申请而不用于限制本申请的范围。
请参阅图1，本实施例提供一种含乙二醇的工业尾气的精馏系统，包括乙二醇储罐10、乙二醇喷射收集器101、第一循环泵11、第一冷凝器12、第二冷凝器21、第三冷凝器22、淋洗塔30、第二循环泵31和活性炭吸附器40。所述乙二醇喷射收集器101设置在乙二醇储罐10顶部，所述第一冷凝器12、第一循环泵11和乙二醇储罐10、乙二醇喷射收集器101相导通。所述乙二醇储罐10顶端开设有第二冷凝器液相回流口102、第三冷凝器液相回流口103、和出气口104。所述出气口104、第二冷凝器21和第二冷凝器液相回流口102 相导通，且所述第二冷凝器气相出口(图中未标注)、第三冷凝器22和第三冷凝器液相回流口103相导通，所述第三冷凝器22与淋洗塔30和活性炭吸附器40依序接通，所述淋洗塔30与第一循环泵11相接通。
所述含有乙二醇的工业尾气直接送到乙二醇储罐10顶端的乙二醇喷射收集器101，同乙二醇喷射收集器10循环的乙二醇进行接触，并与喷射的乙二醇一同进入乙二醇储罐10，所述乙二醇储罐10、第一循环泵11及第一冷凝器12之间由管道相连接导通，尾气中的乙二醇被第一冷凝器内循环喷射的乙二醇降温冷凝回收到乙二醇储罐10中，未凝结的尾气从乙二醇储罐10顶端的出气口104进入第二冷凝器21，尾气中的乙二醇在第二冷凝器21又得到进一步冷凝回收，经第二冷凝器液相回流口102流入乙二醇储罐10，在第二冷凝器21中不凝结的尾气继续进入第三冷凝器22，进一步降温冷凝回收，从第三冷凝器22出来的尾气进入淋洗塔30，在淋洗塔30内进行水喷淋，以捕捉有机物和微小颗粒，从淋洗塔30出口出来的尾气进入活性炭吸附器40进行进一步吸附除杂。淋洗塔30出口还通过第二循环泵31接通至淋洗塔30喷淋入口。
采用上述技术方案提供的含乙二醇的工业尾气的处理系统对含乙二醇的工业尾气进行净化处理的方法，步骤如下：
(1)所述含有乙二醇的工业尾气直接送到乙二醇储罐顶端的乙二醇喷射收集器，同乙二醇喷射收集器循环的乙二醇进行接触，并与喷射的乙二醇一同进入乙二醇储罐。
此时，含有乙二醇的工业尾气温度能从上一个工艺环节出口的150℃以上下降到40-70℃，且尾气中90％的乙二醇会被喷淋捕捉进入乙二醇储罐，40-70℃的乙二醇通过第一循环泵11打入第一冷凝器12降温到20-35℃(得到预降温含乙二醇的工业尾气)进入下一个“喷射-喷淋捕捉”的循环使用。
(2)预降温含乙二醇的工业尾气进入第二冷凝器，然后进入第三冷凝器，工业尾气中的乙二醇被冷凝回收。第二冷凝器用32℃循环冷却水冷却，第三 冷凝器用7℃冷冻水冷却。至此，预降温含乙二醇的工业尾气依次经冷却水、冷冻水换热后分级降温到30-45℃、10-30℃，经过这个过程，预降温含乙二醇的工业尾气中又有部分乙二醇被冷凝回收到乙二醇储罐。
(3)第三冷凝器的尾气进入淋洗塔，进行水喷淋捕捉。淋洗塔上部设有3-9层水喷淋头，水通过第二循环泵实现水的循环喷淋。尾气中有机物被水捕捉。淋洗塔出口污水的有机物浓度较高时进行定期排放。
(4)淋洗塔出来的尾气进入活性炭吸附装置进行吸附除杂。
(5)吸附除杂处理后的尾气按现有方法排入导热油炉焚烧处理。
采用本发明技术方案提供的上述处理系统处理含乙二醇的工业尾气，能将尾气中的有机物浓度降低到5％以下，乙二醇回收利用率为98％以上。
需要说明的是，尽管在本文中已经对上述各实施例进行了描述，但并非因此限制本发明的专利保护范围。因此，基于本发明的创新理念，对本文所述实施例进行的变更和修改，或利用本发明说明书及附图内容所作的等效结构或等效流程变换，直接或间接地将以上技术方案运用在其他相关的技术领域，均包括在本发明的专利保护范围之内。

Claims (10)

  1. 一种含乙二醇的工业尾气的处理系统，其特征在于，包括乙二醇喷射收集器、乙二醇储罐、第一循环泵、第一冷凝器、第二冷凝器、第三冷凝器、淋洗塔和吸附装置，所述乙二醇喷射收集器设置在乙二醇储罐顶部，并与第一冷凝器、第一循环泵和乙二醇储罐相导通，所述乙二醇储罐顶端开设出气口、第二冷凝器液相回流口、第三冷凝器液相回流口，所述出气口、第二冷凝器和第二冷凝器液相回流口相导通，且所述第二冷凝器气相出口、第三冷凝器和第三冷凝器液相回流口相导通，所述第三冷凝器与淋洗塔和吸附装置依序接通，所述淋洗塔与第一循环泵相接通。
  2. 根据权利要求1所述的含乙二醇的工业尾气的处理系统，其特征在于，所述第二冷凝器采用循环冷却水降温，所述循环冷却水的水温≤35℃。
  3. 根据权利要求1所述的含乙二醇的工业尾气的处理系统，其特征在于，所述第三冷凝器采用冷冻水降温，所述冷冻水水温为7-12℃。
  4. 根据权利要求1所述的含乙二醇的工业尾气的处理系统，其特征在于，所述淋洗塔的出口还通过第二循环泵接通至淋洗塔喷淋入口。
  5. 根据权利要求1所述的含乙二醇的工业尾气的处理系统，其特征在于，所述吸附装置为活性炭吸附器。
  6. 一种用权利要求1所述的处理系统处理含乙二醇的工业尾气的方法，其特征在于，包括以下步骤：
    将含乙二醇的工业尾气送入乙二醇喷射收集器，同乙二醇喷射收集器循环的乙二醇进行接触，得到预降温的、且含凝结乙二醇的工业尾气；
    将所述预降温的、且含凝结乙二醇的工业尾气进行冷却，所述冷却为依次送入第二冷凝器、第三冷凝器，得到低温含乙二醇的工业尾气；
    将所述低温含乙二醇的工业尾气送入淋洗塔淋洗，得到喷淋塔尾气；
    将所述喷淋塔尾气送入吸附装置进一步吸附除杂后通过导热油炉燃烧排放。
  7. 根据权利要求6所述的方法，其特征在于，所述第二冷凝器采用循环 冷却水降温，所述冷却水水温≤32℃。
  8. 根据权利要求6所述的方法，其特征在于，所述第三冷凝器采用冷冻水降温，所述冷冻水的水温为7-12℃。
  9. 根据权利要求6所述的方法，其特征在于，所述淋洗塔采用3层以上的水淋洗，优选为3-9层。
  10. 根据权利要求6所述的方法，其特征在于，所述吸附装置为活性炭吸附器。
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